Liquid separation apparatus



April 26, 1949. J. F. HUNTER LIQUID SEPARAT.ION APPARATUS 5 Sheets-Sheet 1 Filed Nov. 18', 1944 INVQUVTOR:

'April 26, 1949. J HUNTER I 2,468,070

LIQUID SEPARATION APPARATUS Filed Nov. 18, 1944 5 Sheets-Sheet 3 INVENTOR. Jcuw-m F. HwvIMu ATTORNEYS.

J. F. HUNTER LIQUID SEPARATION APPARATUS April 26, .1949.

5 SheetsSheet 4 Filed NOV. 18) 1944 INVENTOR."

MZQ Kw+MM BMW-4.56

April 26, 1949. J, F, HUNTER 2,468,070

I LIQUID SEPARATION APPARATUS Filed Nov. 18, 1944 5 Sheets-Sheet 5 I mm n INVENTOR: J awn-2A1 E HwwZIn v BY \mmsm gw -Gwpw/ Patented Apr. 26, 1949 umrso STATES PATENT OFFICE LIQUlD SEPARATION APPARATUS James F. Hunter, New Rochelle, N. Y. Application November 18, 1944, Serial No. 564,108

'18 Claims.

This invention relates to liquid separation method and apparatus, of the kind adapted to operate upon two, or frequently three or more, component liquids having substantial difierences in weight or specific gravity, and in viscosity or resistance to flow, or both, and usually with substantial preponderance in volume of one or more of the several components over the other or others thereof. The combined or associated liquids may be considered as immiscible in the sense that they do not become mixed inseparably or permanently but, whether as suspensions, emulsions or otherwise, are susceptible to classification or separation by gravity or centrifugal action or other decanting operation; and although the liquid-combination to be treated may thus be considered as one of immiscible liquids it may be conveniently referred to as the mixture thereof, in the sense of their temporary mixture, awaiting separation. The field of utility of the invention is wide, but as an instance of the aforesaid class of method and apparatus may be mentioned prior U. S. patent, Hunter No. 2,084,958 issued to this applicant June 22, 1937, showing a separating system designed particularly for handling, for instance, troublesome mixtures and emulsions of tars and oils with each other and with water.

In many industrial processes, economical operation calls for the continuous separation of the fluid components of plant wastes at the current rate of production thereof, so that the several separated liquids may be profitably and advantageously employed, as by recirculation for reuse, and for the recovery of contents thereof that have value as saleable byproducts; and a further reason for separation is to comply with the usual regulations of local authorities adapted to prevent the pollution of inland or coastal Waters.

This invention in one general aspect may be considered an improvement on the method and apparatus disclosed in said Hunter Patent No. 2,084,958, but some of the novel features hereof be practiced independently of the prior disclosure. Specifically, the invention is usefully adapted. as with the prior patent, to the separation of the mixture of oil derivatives and water produced in the manufacture of carbureted water but it is not intended to limit the disclosure to this purpose as it is applicable in the ing the components of separation of any combination of liquids that can be separated by decantation.

For the sake of facility of description the terminology of the gas manufacturing industry is largely used in this specification, descriptively written on the basis of the separation of tar and oil from water, without limitation thereto. As used herein the term "oil is to be considered as designating the lightest liquid in any given liquid mixture or combination, the term tar the heaviest liquid, and the term water the intermediate weight liquid in the combination. In some cases, as in the manufacture of gas, the oil and tar, while immiscible with the water, will mix readily with each other if brought into contact, but may often or usually be maintained as separate or separable entities by the presence of the preponderant water. In describing cases of the separation of combinations of more than three component liquids other designations will be used.

The necessity for breaking any emulsions and otherwise preparing the starting mixture of components for accelerated separation by the usual method of decantation is fully described in said Patent No. 2,084,958 and no further extended reference thereto need be made herein. An important object of the present invention is to provide for the more effective accomplishment of the desired separation, and another object is to accomplish this with smaller apparatus, reduced plant cost and lower operating expense, Other advantages will be hereinbelow set forth. The disclosure of said prior patent involves three method stages, namely, (1) mixing or conditionthe starting liquor; (2) preparatory separation of components; and (3) decantation. The improvements of the present invention are concerned with the entire system but principally with the stage or step of preparation in advance of decantation.

As one feature of improvement the separation is preferably performed in a closed system under the pressure of a pump or other head, and this may be arranged to include the conditioning step. This feature has necessitated certain improvements or structural or operative changes in the mixing operation and unit and in other elements of the apparatus, to the benefit of uniformity and efiiciency of separation.

Before describing the details of the present invention the following preliminary observations are made concerning the principles involved.

The liquid preparatory or separation step is hereinafter disclosed as being carried out in the apparatus unit herein sometimes termed the spiral or scroll element. In form this part may be generally like that of Fig. 11 of Patent No. 2,084,958 which shows in sectional elevation a modified form of scroll element. In the previous disclosure in said patent little attention was paid to this modification of the apparatus. With the addition of the improvements of the present invention this modification is found to be an important feature, being well adapted to several operations essential in the obtaining of optimum separating results.

The apparatus of this second stage will herein be sometimes referred to as the separating ele ment instead of using the term scroll element as used previously, since the action of dewatering the tar is started in it and is carried to a point where the water particles or bodies become increased in size to an extent sufficient to bring about effective gravity separation in the decanter. Substantially complete dewatering could be accomplished in the separating element, but on account of the law of diminishing returns it has been found more practical to complete the separation in a decanter.

The separating element consists of two parts, each having its special duty in relation to or cooperation with the other, and each being capable also of operating separately in the performance of other functions embodied in the complete separating system, with novel aspects of structure and action.

Referring again to Patent No. 2,084,958 the scroll element shown in Fig. 11, as embodied in Figs. 12-15 of said patent, consists of an inlet I5, Figs. 12 and 13, the helical passage I50, Fig. 13, with the liquid withdrawal mouths I53 and I55, these delivering the flowing stream to the spiral passage I05, Fig. 12, which is formed by the convolutions of the membrane or wall I84 Figs. 11 and 12. The spiral passage I05, in Fig. 11, is closed at the top of the passage by the cover I09 and at the bottom by the plate I I I. In this earlier disclosure, the separating element was placed in the decanter, and all of the flow through the separating element passed thence through the decanter which necessarily must be of suflicient capacity to permit the handling of this throughput volume, or else the throughput must be reduced to that volume which could be handled by the decanter without excessive turbulence. In this form of the separating element provision was made for the withdrawal of the tar from the inlet duct at the upper withdrawal mouths and the remainder of the flow was permitted to enter the spiral duct without control.

One of the features of improvement of the present invention provides complete control of the flow through the inlet duct by a progressive modification of the cross-section area of the inlet pasage wherein the area of the passage is reduced at each withdrawal mouth substantially in proportion to the reduction in flow volume clue to progressive withdrawals, whereby the velocity of flow is maintained steady or prevented from falling off to a detrimental extent, and the flowing combination is completely transferred currently to the spiral duct in such manner that the positions of all of the components are controlled and predetermined as the flow enters the spiral passage.

A second improvement feature of this invention provides a means whereby the greater part of the preponderant component (usually water) which may be sufiiciently free from the other components and ready for reuse or for other desired disposal, is diverted from the decanter. Because of this improvement the volume of water necessary for preparation can be circulated through the separating element without necessitating an excessive volume of decanter in order to reduce the turbulence of flow sufliciently to permit effective decantation.

Other improvements in operating methods comprise the following. (3) Ability to separate a combination of more than three components by first breaking down the primary combination into secondary combinations none of which contain more than three components, and thereafter, by the method of this invention, separating each secondary combination into its several components, for desired disposal. (4) In the separation of a combination of three component liquids, where it is desired to withdraw the components as three separate liquids, as for instance, in a watery mixture, the oil and tar separate from each other, the process of dewatering can proceed with respect to all components concurrently and without interference. (5) When one of two components is present only in the form of an emulsion and the gravity differential is insufiicient for rapid separation, the gravity of the emulsion may be purposely modified by introducing into the flow a quantity of a selected separated component, and by causing the emulsion to come in contact and mix with the recirculated separated component, whereby the gravity of the emulsion is substantially altered and rapid separation is made possible.

When the characteristics of the components are such that emulsions are non-existent, or if present are such as will break readily, the size of the separating element can be greatly reduced by the special feature of so re-arranging or reversing the apparatus that the heavier component will be caused to enter the spiral duct at the lower part of the duct and the lighter component will enter at the upper part of the duct, herein accomplished by inverting the separating element and flowing the combined liquids, under hydraulic head, upwardly from an inlet below the spiral passage instead of flowing the combined liquids downwardly from an inlet above the spiral passage.

It is to be understood that in many case the raw starting liquor, as received from the plant, is in a hot condition; which in the case of gas plant waste containing tar is sometimes essential to the fluidity of the tar component; but in other cases the temperature may be that of the surrounding atmosphere.

Because of changing fire and temperature conditions in the usual carbureted water gas manufacturing plant the tar produced varies, through a relatively wide range, in the characteristics that affect the separability of emulsions of tar and water which are formed when the condensable oil vapors, having various compositions, are condensed in an atmosphere of condensing water vapor, that is, excess process steam. Investigation indicates that for the best separating results, each variety of tar has its critical or optimum condition of treatment in the spiral passage, which condition lies within relatively close limits. The treatment condition varies according to the difierence in the Velocities of the components, certain of which components or portions thereof are retarded by friction in contact with the passage wall. As the flow of the preponderant component, usually water, is one of the principal fac-' tors in the preparation process, and since this flow is what causes the flow of the retarded component, the relative velocities are under reasonably complete control in the spiral passage, and the relation between them will vary, for example, inversely with the width of the passage when the height of the passage and the volume rate of flow are constant. By gradually changing the width, and thereby the area, of the passage, the velocity of flow of the preponderant component and there-- by the relation of the velocities of the severalcomponents may be controlled during the traversing of the length of the passage, so that each variety of tar, when several are present, will be subjected to optimum preparation conditions for a greater or less period depending on certain fac tors such as the rate of change of the width of the spiral passage, provided that the required preparation conditions for the various tars fall within the range between the upper and lower limits set by the available flow volume and the area of the passage.

The accompanying drawings show a number of illustrative embodiments of the apparatus and method of the present invention.

Fig. l is a plan view, and Fig. 2: is an elevational View partly in section, both in diagrammatic form, of an embodiment of a complete liquid separating installation, adapted for handling a combination of more than three component liquids, and comprising both primary and secondary separator systems.

Fig. 2A is an elevational View in diagrammatic form of a portion of a modified separating system, in this instance having the pressure-type oi mixer and the upfiow type of separating element. Fig. 3 is a central vertical section and partial front elevation of a modified separating element, corresponding largely with separating element tit of Figs. 1 and 2, adapted for a combination of two components in which the preponderant component is the lighter.

Fig. 4: is a righthand View in section on the line 4-4 of Fig. 3 or Fig- '7 showing the partitions or inner walls which form the liquid withdrawal mouths.

Fig. 4A is a similar section showing. an alternative arrangement of partitions adapted for the. withdrawal mouths for separating a combination or. two components in which the preponderant component is the heavier.

Fig. 4B is a similar section. showing an alternative arrangement of partitions adapted for the separation of a combination of three components in which the component of intermediate weight is preponderant in volume and in which the volume of the heaviest component exceeds the vol ume of the lightest component.

Fig. 4C is a similar section showing an alternative arrangement of partitions adapted for the separation and separate withdrawal of three components in five separate withdrawal mouths for recombination as desired.

Fig. 5 is a horizontal section taken on the line 5-5 of Fig. 3.

Fig. 6 is a horizontal section taken on the line 65 of Fig. 3.

Fig. 7 is a horizontal section taken on the line 1--1 of Fig. 3.

Fig. 8 is a horizontal section taken on the line 8-8 of Fig. 3.

Fig. 9is a horizontal section taken on the line 9-9 of Fig. 3. Fig. 10 is an elevation on a larger scale than Figs. I and 2; of the primaryseparator or assorting unit of helical duct type.

Fig. 11 is a central vertical section of the primary separator of Fig. 10 or Fig. 12, looking leftward.

Fig. 12 is a horizontal section taken on the line t2i2' of'Fig. 10*.

Fig. 13 is a horizontal section taken on the line l'3-43 of Fig. 11.

Fig. 14 is a horizontal central section taken on the line I' l-M of Fig. 15, showing a portion of the transformation section of a separating element having adjustable vanes for regulating the effective area of the withdrawal months.

Fig. 14A is a side view of part of Fig. 14, illus trating' a. means for adjusting the vanes within the transformation section.

Fig. 15 isa vertical central section on the line t5--I5 ofFi'g; 14.

Fig. 16' is a vertical section on the line I6l6 of Fig. 15.

Fig. 1715 a vertical central section of a modified mixing element of closed or pressure type.

Fig. 18: is: a section taken on the section line [8-4 8 of Fig; 17:, arranged with the perforated area at the bottom of the mixing element.

Fig. 18A is a similar section of a mixing element like that of Figs. 17 and 18 but so modified: that the perforated area and the liquid outlet are arranged at the top of the mixing element.

The fOlIOWing description of the various apparatus units, elements and devices shown in the drawings may be first. generally outlined as follows. A separating installation or apparatus as a whole, capable of performing the method of this invention, is-illu'strated in Figs. 1 and 2, these figures illustrating a primary separating or as-- sorting unit 26-, and. two separator systems 21' and: 3! containing respectively secondary separator elements 28 and 3! delivering to decanters 293.1111 32' respectively; while in Fig; 2A is shown a modification of part of Fig. 2, with a system 86 wherein the separating element is replaced by an inverted separating element 36, that is, with upfiowinstead of downflow, preceded by a concliti'oner 33- and delivering to a decanter 9!. The liquid mixturein traversing the primary separator 26 is preliminarily assorted and reassembled into two secondary combinations which next are passed through the systems 21 and 30 respectively wherein is continued the preparation of the components for decanting; it being understood that either or both of systems 21 or 30 could be replaced by the system 86 of Fig. 2A. Following these will next be described the construction and details of the separator elements 28' and 3t, by reference to Figs. 3 to 9, with modifications in Figs. LA, 43 and 40. Next thereafter will be described the primary separator or assorter 26, with reference to Figs. 19.- to- 13. This will lie-followed by a description of a desirable means for adjustingthesizes: or areas of the; withdrawal months or outlets of the separator element, as a part of the control of the general operation, with reference to Figs- 14., 15 and 16. Thereafter will be described the details of the'special conditioner or mixer element 33-, as shown in 2A supplemented by details shown in Figs. 17', 18, and with a modification in Fig. 18A. Following these will be a review or summary of the entire operation of the apparatus including the method steps of the present invention.

Referring first to the general or entire installation, Figs. 1 and 2' show in diagrammatic form, in plan and elevation, a complete separating apparatus adapted for the continuous separation of a combination of two or three, or more than three, immiscible liquid components. The apparatus comprises in general beyond the inlet (a) the assorter or primary separator 26, useful when there are over three liquids, (b) the secondary separating system 21, adapted for the separation of a combination of three components, which includes among its elements a separator element 28 and a decanter 29, and (c) the secondary sepa rating system 30, adapted for separating a combination of two components, which includes a separator element 3| and a decanter 32. With two components either of sub-systems 27 or 30 can be used and the other omitted; while with three components sub-system 2'! alone can be used; in either case the assorter 26 being unnecessary. To so convert the apparatus any suitable valving may be used, c. g. as shown in Fig. 2, the device 45, consisting of a bypass cross-pipe connecting supply pipe 43 directly to the pipe 49 leading to separator 28; with a valve in the cross pipe openable to cut out assorter 26 and separator system 30, and with closable valves in pipe 43 above and in pipe 49 below the cross-pipe. With four liquids the assorter divides the flow into two groups, one containing three liquids, going to separator 28, the other two liquids, going to separator 3|, one intermediate liquid being common to both groups.

Fig. 2A shows a modification of the sub-system 30 for the separation of a combination of two components in which there is included the spe cial conditioner or mixing element 33 driven by motor 34 through speed changer 35, to be further described on Figs. 17 and 18, and in which the separator element 36 is of the upflow type already mentioned with its inlet placed below the spiral passage, otherwise similar to separator 3! to be described.

The flow of initially combined immiscible components from the plant enters the separating system through inlet pipe 31 and is forced through the system by a means to provide forcing head, preferably a pump 38. Pump 38 should be designed to deliver at a constant rate or volume somewhat in excess of the maximum expected production of combined liquids to be separated. The liquid that is required to make up the deficiency in pumped supply is a separated component, usually water drawn from lower overflow tanks 39 or 40, or both of them, through pipes 4| or 42, leading to the pump. The excess overflow connections 39A and 40A of tanks 39 and 40 are placed at a level lower than the initial source of supply 31 of combined liquids to be separated, so that the supply to pump 38 for recirculation is automatically provided, in a manner to make up for recurrent variations in the rate of supply of the starting liquor or mixture. When required to provide greater mass or weight of flow for preparation, the volume of the recirculated component can be increased by increasing the pump capacity, as by pump control means. A mixer preferably precedes the inlet pump 38 or pipe 3?,"

such as that shown in Figs. 1 and of said patent, to condition the mixture for separation; or the conditioner 33 shown in Figs. 2A, 17 and 18 hereof may be used.

The flow of combined liquids passes from pump 38 through outlet pipe 43 to the inlet 44 of the primary separator 26 in which the primary liquid combination is separated into secondary combinations for subsequent complete separation. In

the case shown the division is into two secondary 8 combinations consisting of a plurality of the heavier and a plurality of the lighter components respectively. The operation of the primary separator and of the other pieces of apparatus will be described in detail in connection with the description of the detailed figures.

In the operation of the primary separator the heavier components are withdrawn at the first or earlier withdrawal outlets to disposal pipes 46, ll and 48 (corresponding to NH, I42 and I43 in Fig. 10) which are joined in pipe 49 through which the withdrawn heavier secondary combination is delivered, without rehandling, to the inlet 5| of the separating element 28 in which the components are prepared for decantation. Secondary separating system 21 as noted comprises the element 28 and decanter Z9, and is adapted for the separation of a combination of three components. The element 28 has lower 52, upper 53 and intermediate 54 discharge passages.

The heaviest component in the withdrawn heavier secondary liquid group or combination leaves separating element 28 through withdrawal passage or pipe 52 in combination with a minimum quantity of the intermediate component, and, sinking to the bottom of the decanter, is withdrawn as a separated component through an outlet or mouthpiece 55 and rising disposal pipe 56 to an exterior point for desired disposal.

Similarly, the lightest component leaves separating element 28 through withdrawal pipe 53 in combination with a minimum quantity of the intermediate component, and entering the decanter rises to the top, and leaves the decanter through an outlet 51 and disposal pipe 58, to an exterior point.

The portions of the intermediate component entering the decanter with the heaviest and lightest components, after decanting separation therefrom, is flowed over the edge of the inner tank 6!, below the accumulated floating layer of the lightest component, and descends in the annular passage 59 between the inner tank 5i and outer tank 62, thence passes through space 58 under the inner tank bottom 63, rises through the interior riser pipe 64 and overflows through trough 55 to an upper overflow tank 66 of separating system 21. In said overflow tank the intermediate liquid component is combined with the intermediate component which is withdrawn from separating element 28, free from the heaviest and lightest components, through. withdrawal pipe 54 which leads not to the decanter 29 but bypasses directly to the upper overflow tank,

' where it overflows an adjustable weir 5'! by means of which the quantity or proportion of intermediate component delivered from the element 28 to the decanter along with the heaviest and lightest components can be controlled. The weir in this use of it, where the actions are not static but are kinetic, operates as a means for controlling OI predetermining the resistance to and the flow through the passage 54 relative to the resistances and flows through the other withdrawal passages 52 and 53; whereby the actual velocity and volume of flow in such respective passages is adjustably predetermined, thereby controlling the volume of flow to and through the decanter. The separated intermediate component descends through pipe 68 to the lower overflow tank 39 and either returns to pump 38 by pipe 4! for recirculation or overflows partly or wholly through outlet 35A to other desired disposal, The double tank arrangement of decanter 9 29 is used principally in cases of separation of combinations with which heat must be conserved or added. The hot liquid or water surrounding and underlying the inner tank minimizes the loss of heat from the heavy liquid or fluent tar within the inner tank. The decanter 29 is adapted to separate a mixture of three liquid components and deliver them separately. Its main or inner tank BI is spaced at its side wall from the jacketing outer tank wall 62, providing the downflow passage 59 between them for the preponderating intermediate component; while the inner tank bottom wall 63 is spaced above the outer tank bottom, providing the inflow space 60, leading to a port in the inner bottom wall which delivers upwardly through an uptake passage or riser B l. Said riser extends slightly above the liquid level and into a trough 65 carrying the intermediate component to the upper overflow tank 3.

The separator xit pipe 52 extends through both tank walls 52 and 6| and constitutes the inlet for the heaviest component into the decant- "ing tank 6 l. The separator pipe 53 likewise penetrates both walls as an inlet for the lightest component. The separator pipe 54 bypasses much of the preponderant intermediate component or water directly to the overflow tank 66. Each of the heaviest and lightest components also may have combined with it much of the intermediate component. By the slow decanting action the three components separate in the inner main tank. The heaviest descends and accumulates, and is drawn away, the liquid head assisting, through a .low outlet mouth 55 and uptake pipe as which turns outward, penetrating the walls 5! and 52 to an exterior disposal point. The lightest component rises, floating atop the intermediate component and overflowing by a suitable exit, such as the elevated conical mouth 51,

whence it descends by pipe '58 which turns outward through the decanter walls to its exterior disposal point.

The preponderant intermediate component rises in the inner tank to its overflow edge, somewhat below the mouth 51, and thus overflows, to descend by passage 59 and ascend by riser pipe 64 to the outlet trough as described. The three components are thus delivered separately. The lightest floats high upon the intermediate .and flows out only by the mouth 57 sincethe layer of lightest component is insufficiently deep to be swept over the edge of wall 6| into passage 59. The intermediate component flows over and down in a very slow and quiet manner, having as it does the full circumference of the tank wall Bl' .as its weir; and the velocity of .its overflow is safely insufficient to overcome the decanting force of gravity which holds up the lightest component layer 'buoyantly above the body of the intermediate component.

In the operation of the primary separator 26 the lighter components .are withdrawn at the second or later group of withdrawal mouths,'.being v the lower group due to the downflow, thence passfor decantation. Secondarysystem 311, as noted is arranged for the separation of a combination of two components, as an example of the invention differing from system 21 already described, and presenting, along with assorter 26 and separating system 27, an entire apparatus suitable for handling starting mixtures of four components, one of which will be present in both liquid groups.

The lighter component of the secondary liquid combination leaves separating element 31 and enters decanter through withdrawal pipe 15 in combination with a minimum quantity of the heavier component, and rising to the top of the decanter is withdrawn as a separated component through outlet ii and disposal pipe 78 for desired disposal. The portion of the heavier component which may nter the decanter with the lighter component sinks to the bottom of the decanter and is withdrawn through interior riser "l9 and overflow trough iii to the upper overflow tank 82 of separating system 3t, where it combines with the balance of the heavier component which is withdrawn from separating element 31 through withdrawal pipe '83 and is diverted from the decanter and, free from the lighter component, is delivered to the upper overflow tank 82 over adjustable weir 8t by means of which the quantity of heavier component entering the decanter with the lighter component is controlled. The separated heavier component descends through ,pipe 85 to the lower overflow tank 40 and either .is returned to pump 38 for recirculation or overflows through pipe 40A to other desired disposal.

Fig. 2A shows a modified secondary separating system at in which there is included a mixing element of the pressure type, its details being shown in Figs. 17, 18 and 18A, and in which the separating element 35 is of the upflow type, with the inlet below the spiral passage. In the separation of a combination in which one component is present only as an emulsion, and in which the gravity differential is too small to rapid and efiective preparation and separation, .it is .found necessary to modify the gravity of the emulsion by introducing into the inflowing stream a quantity of a separated component, previously obtained, which is caused to come in contact and mix with the emulsion, effecting the desired modification in gravity. The recirculated separated component to be mixed with the emulsion may be introduced into the inlet pipe 81 (which leads to the driven mixer element .33) at any convenient point; such special inlet and the necessary pump and connections being not shown.

The conditioning action of the closed type of mixing element 33 may be generally the same as was described in detail in connection with the .open type of mixing element shown in Figs. 1 and 5 of the prior Patent No. 2,084,958; the difztere-nces will be described hereinafter .in detail. The combined liquid components .leave the mixer 33 through pipe 88 and enter the central inflet channel of separator element '36 for preparation .for dec-antation. Separator element 1% is indicated as being of the .upflow type, the construction of which may otherwise be the same that or" a separating element of the downflow type to be detailed. In operation the heaviest component is withdrawn at the first withdrawal mouth which in the case of separator element .36 is the lowest mouth, and at a succeeding mouth or mouths if required, so that the heavy .com-

' downfi-ow type of separating element.

easily separated it is possible to shorten the lineal length of the spiral passage with a, consequent saving in plant cost. After withdrawal from separator element 36 the operation of the separating ystem 86 of Fig. 2A is the same as the operation of separating system 30 already described and needs no further explanation as to how the liquids pass into and later from the decanter, except to point out that the heavier and lighter liquids pass from separator element 36 by pipes 89 and 90 to decanter 9| and tank 92.

The general structure and operation of a complete liquid separation system embodying the improvements of this invention having been described, the preferred structure and operation of the respective units of the apparatus will be described in detail, beginning with the separator element 28 or SI or 36, and with special reference to that of Figs. 3 to 9, similar to the element 3|.

The separator element is shown as an improved development of the form of scroll element shown in Figs. 11 to 15 of prior Patent No. 2,084,958. The complete separating element comprises a central inlet channel 93, Fig. 3, preferably a vertical or descending helix, supplied by inlet 96 (corresponding to inlet 15 in Figs. 1 and 2) and enclosed by upright casing I04 (corresponding with inlet unit 93A in Figs. 1 and 2) and providing an annular helical flow passage 93 which at its latter part is continued as a surrounding spiral duct or outflow passage 94, Figs. 3 and 6 to 9, (corresponding with spiral unit 94A in Figs. 1 and 2) and in turn is terminated by leading into a transformation section 95, Figs. 3 and 7. The separating element of this embodiment is arranged for the separation of two components of which the preponderant component (usually water) is the lighter component; and the figures show the The two outgoing passages or pipes of the transformation section 95 are marked I ZIX for the lighter and iZIY for the heavier component and may corre-- spond generally with Withdrawal pipes I6 and 83 of Figs. 1 and 2. The described parts provide a closed continuous passage from the inlet pipe 9 6 to the outlet pipes I2IX and IZIY. By the progress of the helical and spiral portions of the passage about the axis of the element the mass of the stream travels revolubly and so affords a differential action or classification of the component liquids of differing densities, the heavier taking the more outward paths or lanes by their greater centrifugal force.

Referring further to Figs. 3 to 9, the helical inlet channel 93, in which occurs a revolving or whirling fiow, extends from the inlet 96 to suecessive Withdrawal mouths 91, 98, 99 and I00, discharging :at different levels into the spiral duct.

The channel 93 is constituted of the space enclosed by the cylindrical outer casing I04, the successive convolutions of the helical membrane or enclosed Wall I03, and the wall of a central upright inner pipe I enclosing idle or dead space. The mode of formation of the successive withdraw-a1 mouths 91, 98, 99 and I00 by the differential positioning of spiral membranes or walls I06, I07, I08 and I09 respectively, Figs. 6, 7, 8 and 9, and the continuation of all of these membranes as the common membrane II2, which forms the wall of the spiral passage of the separating element, are generally described in the prior Patent No. 2,084,958 at page 5, column 1, line 73 et seq., and will be here further described.

' Referring first to Fig. 3, the first or top cover plate II4 of the spiral passage 94 is attached to the outer casing I04 of the helical inlet duct at the level of the top of the first or highest withdrawal mouth 97. At said first mouth 91 and continuing therebeyond in the convolutions of the helical inlet duct, the outer casing or wall I04 as such is discontinued. Also, at the first withdrawal mouth 91, Figs. 3 and 6, an upright membrane I06 starts, spaced inwardly from the position of wall I04 by the desired width of said first withdrawal mouth. Membrane I06 is attached at its top and bottom edges to the under and upper faces respectively of one turn of the helical membrane I03 which is the helical septum that forms the successive convolutions of the helical inlet duct 93 and also forms the top and bottom walls of the successive withdrawal mouths. The fourth or closing side of the first withdrawal mouth 91 is the inner end of the spiral membrane II2, Figs. 3 and 6, which extends upward and downward to and is joined with the respective cover plates I I4 and I I5 and is the septum which forms the succeeding convolutions of the outwardly trending spiral passage 94. The outer casing or wall I04, Figs. 3 and 6, in the convolution of the helical passage 93 preceding the first withdrawal mouth 91, terminates at the first withdrawal mouth 91 where it merges with and continues as part of the membrane II2, completing the four-sided enclosure of the first of the withdrawal mouths that discharge from the helical convolutions into the first spiral convolution.

The upright membrane I06, Figs. 3, 6 and 7, continues through a single convolution of the helical inlet duct, between convolutions of wall I03, forming a helical spiral in which the distance from the central axis increases by the width of the first withdrawal mouth. Membrane I06 extends to the second withdrawal mouth 98, Figs. 3 and 7, where it merges with and continues as part of the spiral membrane I I2. These formations trend downwardly but in the separating element 36 of Fig. 2A would trend upwardly.

Similarly, succeeding withdrawal mouths are formed at the succeeding convolutions of the helical inlet duct by membranes I01, I08 and I09, Figs. '7, 8 and 9 respectively. Membranes I0! and I08 are incorporated in the structure in the same manner as described for membrane I06. These membranes start at their respective withdrawal mouths, and. each terminates at the succeeding withdrawal mouth, whereat they each merge with and continue as membrane I I2, between the convolutions of which occurs the confluence of the streams delivered from the helical to the spiral duct through the several mouths I06 to I09. Membrane I09 starts at the last, in this instance the lowest, withdrawal mouth I00, Figs. 3 and 9, and it extends from the last helical membrane convolution I03 to, and is attached to, the second or bottom cover plate H5; and membrane I09 terminates at the point where the membrane I08 merges with membrane II2 which is also attached to cover plate I I 5 as described. The forms of the membranes I06, I01, I08 and I09 are helical spiral curves in each of which the distance from the center or general axis increases by the width of the respective withdrawal mouths, and which curves extend preferably through one single convolution or 360. The spiral duct 94 preferably has increasing area of cross section, for a number of convolutions, and at its outer end passes by way of continuation section II6 to the transformation section 95.

An advantageous further feature of the present disclosure is the introduction of an inner wall 313 :rinembrane-i 113 1 of spiral and helical; character, ij'liigs. 3 and to 9, which startsat the wall ofthe :central vertical pipe -1|'05 in the same convolution with and in theradiahplaneof the startof the membrane.il05. that forms the first withdrawal mouth 91; and trendsdownwardly and outwardly. :Membrane H3 thusv continues through the several final convolutions of-the: helical duct 93,-. ext-tendinglbelow the top ;Q1 osure: wall I I4, and in which the withdrawalmouths areplaced, and lies :.concentric with.;membranes-lll6, 7101 and 108 nwhich form the earlier. mouthsv in the series-of uwithdrawal mouths, and .ends;.at the; start. of ,membrane iU9,,Figs.;3.and 9, which-tformsithe .last withdrawalzmouth i100, and to which memtbrane I69 the membrane H3 is joined'so' that imembrane 1W9 becomes the continuation and termination otmembrane 113. .In each convolu- 'tion, in the lower end of the separating element,

the distance between thewall of central pipe I105- =1 and the membrane H3 increases by the extent eof the width of thewithdrawal mouth in that convolution of thehelicaluduct 93, so that the -tarea of the fluid passageway or helical duct is substantially proportional with the volume of .centrifugalforce are sustained to the end, to the ximprovementpf. the classification of the'liquids -:before being withdrawn into the spiral duct. Like :"the space within the centralstandpipe )5 the space within the helical-spiral inner membrane wall H3, between it and the pipe 105, is an idle or dead space, exterior to which the active ducts n are disposed.

The spiral passage 94,:within which thewhirl- -ring or revolving'flow continues, is the outwardly "trending space enclosed between top wall H4, bottom wall H5 and the successive convolutions of the spiral wall or membrane H2; and said spiral membrane H 2 is joined to and becomes the continuation of membranes NIB, I01, I08 and .109

:which form the withdrawal mouths of the helical vinlet duct-93. Said top cover Wall or plate H4 is attached to the outerwall N4 of 'thehelical inlet duct. Thetop cover plate IM- and bottom plate H 5 are attachedto the top and bottom edges respectively of the spiral membrane H2 through-.

. out its length so that the spiral passage 94 forms a closed continuation of the closed helical inlet duct 93. The sectional area of the spiral passage 94 varies with the width of the passage, the

Y heightbeing constant, and it can be designed or adapted to produce any desired velocity condition with constant volume of flow.

The spiral passage 94 terminates where, at -tangency,.it runs into the inlet section H8 '(Fig. of the transformation or withdrawal section 95. The inlet section H6 is a relatively short tangentpassage enclosed by and between a continuationof the spiral membrane H2, an op- -posite vertical membrane Ill, attached to and forming the continuation of the convex side of the next inward convolution ofthe spiral membrane 112; an extension of thetop cover plate H4 and an extension of the bottom plate H5. The inlet -section- H6 "and the-transformation -*-section-'95; together,-= are: sometimes referred to .--'.he ei aas h i is osal sectio nofethe sep ratin element; 1 and here the whirling, .fiow Which ;.has continued from element inlet. r96 to its outlet 1 l6 becomes transformedinto advancing flow toward the decanter.

is. divided by;one;.or.moreymembrane partitions into separate withdrawal months for the division and. withdrawal of; :the several; classified portions of the flow.

Fig. 4 shows; arighthand viewjn section on the .line 4-4,of'Fig.;3 orI-Fig. 7. .Thearrangement shown in this view is preferred forfthe transformation :1 section .pf a ,=.,s eparating ;';.ele.ment

adapted; especially: ior the: separation; of av combination of two componentsin which the preponderant component..- iswthelightcr. The parti- 1.tionst l2! suitablyzdividegthe flow.;=.of..the stream.

component which zhas zbeen 2. moved .outward The .L-shape channel .l2;lY receives the, heavier centrifugally andgdownward: gravitationally;.;zthe

:remaining, channeL Li 2 5X receiving .the, preponclerating lighter component.

.- Fig. 4A shows;a.:.modified;partition. -l2.l.A,;in a

sectional view corresponding with; Fig.;.4i:. of .the

- transformation; section of. a separating. element adapted for .the 'separationiofiacombination of .two components inzwh-ichxthe prenonderant component is the heavien. .Itsg-dispositionand action I are the reverse of .thoseof Fig. 4.

Fig. 4B shows. a further. modified partitiomarrangement 121B; atthe same .sectionahposition, u of the transformation section. :of a2; separating element adapt-ed forithe separationof a combina- .tion of three components; which the :intermediate Weight componentisz.preponderant.in volume. It. provides a large oentra1..channel 120 ior the intermediate component surrounded by peripheral. L-shape.- channels corresponding '1 to those of Figs; 4- and 4A.

' Fig.- 4C. showsanother modifiedxpartitiomarrangement i210, at the; same sectional position,

with a simplified construction of the transformation section. .The respective. disposal pipesingthis case canbe selectivelyt-connected so, asxtoirecombine the withdrawn components in difierent ways. as desired. Means for adiustment. arezdisclosed in Figs. i l-and 14A.

The upright .centralportionpr element of the separator 28,.whichcontains the helical. channel 1.93, is marked 93A, and thexenlarged;portionthereof containing the spiral duct 9 iisn'iarked MA; on

, the drawingsyand .the corresponding portions. of

separators 3i and 36 aresimilarly designated,.on

-Figs. 1, 2 and 2A.

In operation; the .flow'in' the helical duct-:93,

throughout its; closedoutside orupper. section and its inside .orcdiseharging section, is :main- "the enclosing wall 164 and the 'lightest at the in- ;nermost layer....against- ;the-wall of; central pipe or standard IE5, or, .further aong in this instance,

lower down, against themembrane. l-I3after the first withdrawal mouth 91 .hasheen passed. vThe heaviest component beingv against the outerrwall 5 m4 is withdrawnfirst; namelyby thefirst-mouth,

or bythe earlier'group of mouths'in the-series of Withdrawal mouthsgjfnthe"Volume 40f v:the heaviest component is toos great;.and .thus enters the spiral passage 94. at its top-portion incontact with the outer or concave wall H2 of the spiral passage, being a continuation of membranes I06Itl9. The action of the flowing portion or component of intermediate weight, which exists from channel 93 by the next mouth or group of mouths, in spreading, rolling and kneading the heaviest component as it is caused to traverse the spiral passage, descending across the spiral membrane II2 as it is moved along outwardly by the flow, is fully described in prior Patent No. 2,084,953 at page 5, column 1, line 28 et seq.; and th erosive action of the flowing stream in breaking the accumulated globules is there also fully described.

Similarly the lightest component takes its place against the inner wall I65 of the helical duct and is withdrawn at the final group or at the last in the series of withdrawal mouths, and so enters the spiral passage 93 at its bottom part, in contact with the inner or convex wall H2 of the spiral passage, and is subjected to the action of the flowing stream as it rises across the spiral membrane I I2 while being caused to traverse the spiral passage. The component of intermediate weight is withdrawn by the intermediate mouths and takes a middle position between the heaviest and lightest components, in entering the spiral duct.

The position of the several components, whether two or more in number, entering and traversing the spiral passage is such that the preparation for decantation proceeds concurrently and without interference, with respect to all components. The final classified arrangement of components, two or more in number, progresses from the spiral duct to the transformation section 95, and thence at least partly to the decanter. The details of the transformation section 95 will next be further described.

In Figs. 3, 4 and 7 is shown a partition I2I, which subdivides the transformation section 95 into two channels. This partition is L-shaped, having vertical and horizontal portions, and it starts in the inlet section III; relatively close to the start of the transformation section 95. The arrangement shown is designed for the withdrawal of the components of a combination in which the lighter component is preponderant in Volume, wherefore the larger channel is at the upper and inner part of the entire flow area. Fig. 4A shows the modified arrangement with an interior partition I2IA subdividing the transformation section into two channels for the withdrawal of the components of a combination in which the heavier component is preponderant in volume. Separator element 3|, Figs. 1 and 2, requires the partition arrangement I2 IA, Fig. 4A, the channels terminating in pipes 16 and 83 as previously described. In Figs. 3, 4 and '7 the partition IZI forms two channels, which are continued as disposal pipes I2IX and I2IY, the former to accommodate the preponderating component. The partitions I2IB and I2IC, Figs. 43 and 4.0 have already been described.

It will be understood that the section 95 beyond the scroll outlet is a walled member or chamber in which the entire flow is transformed into subdivided streams apportioned approximately to the expected volumes of the respective components, the chamber being interiorly partitioned in one way or another for this purpose.

Describing further the embodiment of Fig. 4B which shows the arrangement of withdrawal mouths for the separation of a combination of three component liquids, in which the preponderant component is the intermediate weight component, and in which the volume of the heaviest component exceeds the volume of the lightest, the general position of the component liquids entering the inlet II6 of the transformation section is as follows. The heaviest component will have reached the bottom of inlet passage IIS, or is partially placed upon the side of the extension of membrane II2 if, in traversing the spiral passage, it has not completed its downward travel across the width of membrane II2; the lightest component is at the top of the inlet passage H6 or is placed on the wall II? which forms the extension of the inner or convex wall of the spiral passage 94; the intermediate weight component, being the balance of the flow, occupies the balance of the area of inlet passage I I6.

The withdrawal outlets of the transformation section 95 modified as in Fig. 4B, formed by the partition or septum I2IB, are adapted to receive the components in the same arrangement as supplied by inlet II 6. Thus, withdrawal outlet or channel II8, including the area at the bottom and along the eXtension of spiral membrane H2, is designed and dimensioned to receive all of the heaviest component and a minimum quan tity of the intermediate weight component. Withdrawal outlet I I9, including the area at the top and along the membrane I II which forms the extension of the convex or inner wall of spiral passage 94, is similarly designed to receive all of the lightest component and a minimum quantity of the intermediate weight liquid. Withdrawal outlet I20, including the balance of the area of the inlet section H6, is designed to receive the balance of the flow, which comprises substantially all of the preponderant intermediate weight component, including both primary and recirculated separated intermediate component, free of the heaviest and the lighest components and ready for desired disposal. Each withdrawal mouth I I8, I I9 and I20 is connected to a separate disposal pipe. As an example separator 28, of the separating system 21, at the righthand sides of Figs. 1 and 2, requires the partitioning I 2IB of Fig. 4B, the channels being continued as pipes 52, 53 and 54; the intermediate liquid, as water, flowing by pipe 54 direct to the upper tank 66, and thence to the lower tank 39 as before described.

In Figs. 3 and. 5 to 9 the membrane H3. which in this embodiment trends downwardly and outwardly to effect the progressive decrease of area and volume of the descending helical channel 93 as already explained, at the same time demarks or bounds a progressively increasing space enclosed between the membrane and the central standard or cylindrical wall I05, growing from zero area at level 6-6 to the full sectional area between wall I65 and spiral wall I09 at level 9--9; and this enclosed space, like the space enclosed inside the wall I05, is an idle or dead space, subtracted, for the purpose of coordinating the channel area with the decreasing flow, from the otherwise full area shown in the prior patent, Fig. 13. Thus the whirling velocity and classification are maintained.

When the characterstics of the component liquids do not present such conditions that extended preparation in the spiral passage or duct 94 is required to eilect separation, the length of the passage to provide time for the components to traverse the vertical width of the spiral scroll or membrane II2, Fig. 3, can be reduced, which in turn reduces the necessary size of the separator element 28, 3| or 36 and its cost. To the aeoaovo same end the placing of the components as they pass from the helical inlet duct or channel .93 to the spiral pas a or duct 94 may be the re verse of the arrangement described, the heaviest component being delivered into the spiral Passage at its lower part, whereat it continues throughout its travel through the spiral passage, and the lightest component being placed at the upper part of the spiral passage where it continues. The separator element 36, Fig. 2A, shows the inverted arrangement to accomplish this result. The construction of separating element .36 may be otherwise as shown in Figs. 3 .to ,9. The element is positioned .so that its inlet :section 93A rises from below the spiral passagesection 94A, and the flow in the inlet channel thus is upward, which is the reverse of the positioning of the separating ele ments 2.8 and 3|. With upfiow operation, the several components are caused to be placed in the flowing stream in the inlet channel 9.3 in the manner as described for the downfiow type of separating element. The heaviest component moves outwardly and becomes positioned at the concave outer wall L04, Fig. 3, and thus is withdrawn at and by the first mouth or by the first group of mouths in the series of withdrawal mouths, which in this .case are the lower mouths, and is thus delivered into the spiral passage at its lower part. The lightest component, becoming placedat the inner wall 1.05 .and then wall I I3 of the inlet duct, is withdrawn at the final group or at the last in the series of withdrawal mouths, which in this case .are the higher mouths, and is thus delivered into the spiral passage at its upper part. Separator element 3.6, Fig. 2A, for the separation of a combination of two components in which the lighter component is preponderant in volume requires a transition arrangement such as that of partition .1251, Fig. 4, the Partitioned channels terminating in a 1 31 8 89 delivering die root to the decanter 9i and a pipe 9.0 delivering to an upper oyerflow tanls 92 and lol -passing the decanter 9|.

The primary separator or assorter 26., Fi s. 1

and 2, is shown in detail in Figs. 1,0 to 13, Its

function is to handle a multiple mixture, e. g. 4 or .5 components, and assert the components into r ps of three or less liq ids each, by specific gravity, for flow to and separation in two or more secondary separators, ne for each liquid group. The construction and operation of the illustrated assorter is principle substantially the same s the described helical inlet duct portion of one of he separator elements. 28, 31 or .35 considered as far as its withdrawal outlets, omitting the spiral scroll portion thereof.

The helical duct 122 of the assorter 2B is the space enclosed by the outer shell or casing 123, and the successive convolutions 0f the helical 'inembrane I24 and the inner or central cylindrical wall .or pipe .125. Withdrawal mouths 1.2.6, I21, I28, .129, I30 and I.3I are formed by the posi- .tioning of upright membrances 43-3,, I34, I35, L36, I31 and I38 respectively, he inner membrane I 38, corresponding with wall M3 in Fig. 3, starts at the wall of the pipe I25 in the same con.- volution with andin the radial plane of the start of the first upright membrane ;I-33, which latter forms with the outer wall I23 the first mouth I26 in the series of withdrawal mouths. Mem- .brane I38 continues throu h, several convolution-s concentric with membranes I33, I 34, L35, r1135 and I31, .form the successive withdrawal mouth-s I26 to .I.3.I .in the several .convolutions, and terminates at the last mouth I31 in the series of withdrawal mouths, which mouth [3| is termed between membrane I38 and membrane 131. Thus by the disposition of membrane 138 the descending annular helical channel progressively decreases in area correspondingly to the decrease of flow beyond the successive mouths, .maintaiu ing flow speed. The membrane I38, like mem brane I I3 of the separat r. encloses between it and the central cylinder L25 a progressively wid ening space which, as well as the space inside of the cylinder, is a dead or idle space. Structural-1y en al cyl nder or empty shait m ybe the support or base upon which, as by tight fitting, attaching or welding, the various other walls of the helical element may be mounted.

The successive withdrawal mouths I26, I223, 118, He, 1.3.0 and 131., sh wn as arran ed ex dus of three are connected respectively to pipes @MEI, I42, I43, I44, I45 and I45 by m ans of transformation pieces interposed between the mouths and the pipes. This const uction is in cheated by transformation pieces I41 and I43, Big. 2 and at I49, Fig. 13. leading resp c ively into pipes I42, I44 and M5.

The operation of the assorter or p ty separator is similar to the operation of the helical inlet duct portion of 1a separating element as al. eady des ribed. The portion of the with drawn by each in the series of withdhawal mouths 426 to I3! isdeliv red loy its transformation phase to a separate one of the disposal pipes IM to Mi. These withdrawn ortions of the how are rec m -incd in groups into sec ndary combinations .for subsequent complete separation. Referring to primary separator 26, Figs. 1 and 2, the grouped disposal pipes .6,. 41 and 4.3 (or in Else 1:9 1 i es II to I 43) are co nected thefi st or earlier .group in the series of withd awal mouths and are there eyond unitedas the p e 4.9 th ough which the heavier secondary combination-41s [doe llYGI'Bd to the separating element .28 of the first separation system :23. Similarly the disposal pipes -'I I, 12 and 13 -(or in Figs. 10 to P13, pipes M1! to I46) are connected to the second or later roup in the series of withdrawal mouths, and are therebeyond united as the pipe M, thnough which .the lighter secondary combination is deliuemd to the separating element 3I of the second separatin system 3.0.

It is to be understood in regard to the primary fidparator .or assorter .216 that it may he onenated with either downfiow or :llpflow of liquid the helical channel, in the same sense as already described in connection with the inlet channel members of the secondary separators, which in volve downflow in Figs. .1 and 2 and upfiow in Fi 2A.

Under certain conditions of operation, variations in load, eith r sea onal or -for-other causes. are of such magnitude that it becomes advisable to adjust the effective areas of the withdrawal mouths in the respective .transliormationsections of one or more of the separating elements .35 or 36. Figs. 14, 15 and 16 showan illustrative ar .rangement for the purpose, comprising adjustable partiticns or vanes ital, J52, 1:53 and I54 swung by control shafts I 55., 1.5.6, iI5'I1and 1.5a .spectivelyh se vanes .n spectively are c ntim uations in line with ,fixed partltion walls 1.9.1., 32,. 1-93 and 19.4, beyond. which the walls are harmed to pr de separate channels. These pa titions correspond with fixed partitions 1M0. in Fig. 41.0. The control shafts are extended through the walls of the transformation section and through stuns ins b xes and glands 196, of :usual ,type and are regulated by levers and locked. For example, each shaft may be turned by a hand lever I91 to a selected position and the adjustment fixed by means of a segment I98 formed with an arcuate slot I99 engaged by a nut-and-bolt device 2% on the lever, by Which the lever, shaft and vane are secured in their adjusted position.

The figures indicate an inlet section I I60 leading to a transformation section 95C, analogous to those shown in Fig. 4C having a central channel I28 for the preponderant liquid component and four surrounding channels MI, 262, 283, and 204, for a case wherein separation between up to five liquids is desirable. Figs. 14 to 16 indicate the five channels, and for each surrounding channel a regulating vane such as those numbered I5I to I54. Each vane is in line with an inner or partition wall of an outgoing channel, and is so pivoted to or near the wall that its free end may be swung in the advancing stream of classified component liquids, to cut off adj ustably a greater or lesser thickness of layer of the general flow stream. Having knowledge of the expected proportions of the components the vanes, by their shafts and adjusting means, are set in a way to separate away from the total stream each of the components, other than the main or central component, and direct it into its proper outgoing channel, as nearly as may be done to thus divert each component, to the maximum extent and with minimum mixture of another component and direct it into its designated outgoing channel, leading to a separate pipe conveying it to its intended position in the decanter portion of the apparatus.

In operation, the shifting adjustment of the vane or partition I5I, for example, toward the inlet bottom wall II5 of the inlet or transformation section decreases the area of withdrawal mouth of channel 28I while increasing the area of the central withdrawal mouth I28; and adjustment of the partition I5I in the opposite direction or inwardly reverses such area change with respect to the two withdrawal mouths affected. Similarly the swinging of partitions I52 or I53 or I54 toward or away from the exterior walls H4 or H2 or II1 of the transformation section will affect the areas of the withdrawal mouths of channels 262 or 263 or 264, and as well the middle channel I of the predominant component. Increasing the effective area of the withdrawal mouth of the central duct I26 of course increases the volume of separated preponderant component (usually Water) which is diverted from entering the decanter, thus resulting in reduced fiow through the decanter and more effective separating and decanting operations.

A mixing element or device of substantially open type and motor driven is illustrated in the prior Patent No. 2,084,958, located in the inlet to the separating element. It is found preferable in some instances to maintain pressure within the mixer, and a-closed or pressure type of mixing element 33 is herein shown in Fig. 2A, and in detail in Figs. 17, 18 and 18A. It comprises, within a built-up housing I1I-I11, an inlet chamber or section I6I, enclosed by a housing portion or shell I12, and its left end head I13; and an outlet section or receptacle I63 for solid materials, enclosed by cylindrical shell I16 and right end head I11; and an annular outlet chamber or section I62 for liquids, enclosed by shell portion I1 I and separated from inlet section I SI by a diaphragm or partition I68 and separated from outlet section I63 by diaphragm or wall I69. Sur- 26 rounded by the annular chamber I62 is a cylin drical perforated or screen member or membran I64 having its ends fitted within the annular diaphragms I68 and I69 and attached to diaphragm I68 by angle ring I16.

The cylindrical screen may be of mesh or other perforated sheet material and it encloses what may be called the mixing or screen chamber I556. The screen preferably is not completely perforated, but only at selected portions. Thus in Figs. 17 and 18 the perforated area IE1 of the screen membrane I64 is shown placed at the bottom. The mixer contains also a driven mixing and feeding device. A helical Wiper blade I65, mounted on shaft I66, has its peripheral edge substantially contacting but preferably closely spaced from screen membrane I64, and it is operated by a motor 34 through a reducing gear indicated as 35, as seen in Fig. 2A. The shaft I66, Figs. 17 and I8 extends through the mixer head I13 within stuffing box I14 and gland I15, and extends through head I11 through stuffin box I18 and gland I19.

The flow of the stream of combined liquids to be separated enters the mixing element through inlet pipe I8I of Fig. 17 or B1 of Fig. 2A. When it is necessary to introduce into the flow an added liquid, such as a separated component, especially for mixing it with an emulsion contained in the mixture, in order to modify the gravity of the emulsion, the introduction can be at any point along pipe I8! as by lateral pipe I82. The pump and connections for handling the introduced or recirculated liquid or separated component are not shown. As a liquid outlet there is shown downtake I83, or 88 in Fig. 2A, and an outlet I84 is provided for solids, if present, the mixer screw I65 acting as a feeder thrusting solids rightwardly toward the chamber I63 and its exit 584. The solid outlet I84 is shown as a downtake pipe or passage having upper and lower discharge or dump valves I85 and I86, with a collecting space or section I81 between, from which received solids can at desired intervals be discharged.

The perforated area of screen element I64 is relatively large so as to reduce the velocity of flow through the perforations and to provide a greater length of time in which to effect contact and mixing of liquid components, these actions being substantially as explained in said Patent No. 2,084,958. Also, illustrative details of the perforations and clearances are described in said prior patent at page 4, column 2, line 6 et seq., and the method of operation at line 27 et seq. The present construction of conditioner or mixer is an improvement in its closed and sealed housing, its internal pressure and otherwise. The reducing means for the more viscous liquid comprises a screen and wiper device, the screen being a perforated cylindrical wall inside an annular chamber, adapted to break up and shred the viscous masses or lumps thereby releasing therefrom a less viscous liquid or liquids, while bringing together different portions of each component.

In Fig. 18A is shown a view in vertical section similar to Fig. 18 of a modified mixing element, in which the perforated screen area I88 is placed at the top. The placing of the perforated area at the top or at the bottom of the cylindrical screen membrane is determined by the characteristics of the liquid components to be separated. Usually the perforated area is more advantageous at the bottom, as the heaviest component, tar, exceeds in volume the lightest component, oil, and is also the most viscous, and the most in need of escapee The g n ral m hod of operation may now be reviewe upo th en ral showin of pparatus in Figs. 1 and ;2 by assuming the continuous upplyin y pipe 3 of a hot starting liquor composed for example of water in preponderance and, for exampl two heavier components or tars of ldilferent gravity, and one lighter component or oil. The pump 38 may e of a type deliverin the progressive now at a pred termined or fixed rate, any deficiencies of supply, as of water, for recirculation being made up from tank 39 or 43 yway of p pe an or 2- The pump output passes through the primary separator or assorter 26, needed only because there vare over three components. It groups the heaviest three, delivering and merging them through single pipe #39 to the {f rst secondary separator 28, and groups the lightest tWO, Passing them by pipe M to the sec.- ond s par r 3 water t us passing to both separators. If there be emulsions, or .tar masses embedding water or-oil or both, there should be a conditioning operation before separation; and the closed conditioner 33 of Fig. 2A may be used, for example in advance of the separator 28, or better, ahead of the assorter 26; but if conditioning ahead of the pump is desired the open type of conditioner of said prior Patent No. 2,084,958 may be substituted. In the separator 28, both in its helical inlet channel 93 and its succeeding spiral .duct 94, Fig. 3, by whirling or revolving motions during progress of the flow and by gravity operation in the duct, effective classification is per.- formed, and the transformation section 35, Figs. 3 and '7, receives the issuing components arranged according to their gravity, and may deliver them accordingly directly into a decanter as in the prior patent; but herein the 110W is shown as subdivided by partitions or septa, arranged according to ex-- ,pected volumes, delivering respectively into separate pipes or passages 52, 53and 54, at least two of which then deliver into the decanter 29 having a tank of such volume as to give each portion of the flow ample time for more complete separation ,of the three components, to be taken off by separate decanter outlets, as explained. With a properly designed and dimensioned flow transformer or transition section 95, the intermediate component may be largely withdrawn by pipe 54 in a condition free of the heaviest and lightest components, and therefore ready for disposal or recirculation without going to the decanter; and each of the heaviest and lightest liquids will then .carry a variable proportion of the intermediate liquid, so that the decanter receives all three, but in a gross Volume reduced by the bypassing of the bulk of the intermediate componet, including original supply and recirculated component, a practical advantage permitting the recirculation of larger quantities, for better elliciency, without increase of decanter size. The intermediate liquid may be conducted to the overflow tank 3. 9, for use .or disposal. In special cases the separation of components in the helical and .spir.ai1 passages! separator may be suifieiently complete to permit disposal Withoutgthe need of later decanting, since much gravity action occurs in the spiral duct, which may be prolonged to a further extent for this purpose. The components passing from the :assorter 26 to the second separator 3| may undergo .operations analogous to those just described. The final result of passing the initial liquor through the described stages or steps and units of apparatus, is its efiective subdivision into its components ready for industrial utilization or other disposal.

There have thus been described liquid separaion met od and apparatus embodying the print ciples and attaining the objects of the present invention. Since many matters of operation, com!- bination, construction and arrangement may be variously modified without departing from the discl sed principles it :is not intended to limit the invention to such .matters except to the elltent set forth in the appended claims.

I claim:

1,. Apparatus for continuously separating .a, flowing liquor consisting of .a mixture of liquid components of difliering ravity and viscosity, ha g a eparator tor classifyzin the component i t comprising a central u right inlet element and surrounding it an elongated spiral.- walled duct traversible outwardly by the liquid flow with the heavier component advancing and descending progressively in contact along the concave duct wall sunfaee for delivery at the lewer P of e sp a Walled duct and with lighter liquid delivery thereabove; said central inlet element comprising an axial standard and. a helical annular wall forming .a channel surro d n said axial standard and composed of an exterior section followed by a section inside of the spiral Walled duct, connected liquid tightly to said duct, the oonyolntions of the exterior section being closed and acting to impose whirling and centrifugal classifying motions upon the flow, and the inside convolutions being formed with successive take-old mouths adapted to skim ,ofi from the whirling flow and deliver into the spiral duct first the heavier and later the lighter liquid components; and saidinside section having a helical-spiral wall arranged to decrease progressively the helical channel sectional area thereby to maintain substantial flow speed and whirl as the flow volume decreases beyond the successive talgeoil mouths; and wherein is .a flow-transformation walled member into which the spiral duct .de. livers and formed with partitions subdividing it into separate channels for the outfiowing components and proportion-ed to the expected vol? umes thereof; with movable yanes for relatively adjusting the partitioned channels to the flow of the respective components.

2. Apparatus for continuously separating four or more liquid components of differing density and viscosity from a flowing mixture thereof, including a primary :assorti-ng element comprising an upright helical duct member having in succession liquid classifying and delivery sections of substantial extent and formed with a closed outer shell and an axial standard and a helical interior wall defining the helical duct, and formed at its delivery section with a succession of peripheral take-01f mouths delivering at successive elevations from the helicalduct, a series of at least four separate .fiow passages receiving from the respective take-off mouths the classified components, said passages being combined in at least two groups with a plurality of passages in each group, a secondary separating element to which the first passage group conducts its entire flow for further separation and a second secondary separating element to which the second passage group conducts its entire flow for further separation; said apparatus including also, beyond the respective secondary separators, decanters receiving classifled components therefrom; and said secondary separators having delivery bypasses for a preponderant component each disposed to conduct such component to bypass the decanter.

3. Apparatus for continuously separating the liquid components of differing density and viscosity from a flowing mixture thereof, comprising a decanter for final separation and, in advance thereof, a spiral-duct separating element operating by centrifugal action and gravity for classifying, rearranging and delivering a plurality of components at predetermined positions in the flow stream, and as a continuation of said spiral duct a walled transformation chamber having partitions forming separate flow channels positioned respectively to receive the classified components in their aforesaid flow positions and with their effective entrance areas proportioned to the expected volume of the components; and passages therebeyond conducting the flow from selected ones of such flow channels to the decanter to conduct a combination of components thereto in predetermined positions in the decanter.

4. The apparatus as in claim 3 and wherein the subdividing partitions in said chamber are provided with movable vanes at the entrances to i such channels, and exteriorly accessible means to adjust each of said vanes to vary the channel entrances to accord with the expected volumes of components.

5. Apparatus for continuously separating the liquid components of differing density and viscosity from a flowing mixture thereof, comprising in advance of a decanter a spiral-duct separating element operating by centrifugal action and gravity to classify a plurality of components and deliver them at predetermined zones in the flow stream, and following said spiral duct 2. walled transformation chamber having partitions forming a plurality of flow channels positioned respectively to receive the classified components from their aforesaid zones, said partitions having adjustably shiftable vanes at the chamber entrance whereby to proportion the effective entrance areas of such channels substantially to the expected volumes of the components; and passages therebeyond conducting the flow from selected ones of such flow channels to predetermined positions in the decanter.

6. Apparatus for continuously separating the liquid components of differing density and viscosity from a flowing mixture thereof, comprising a decanter for final separation and, in advance thereof, a spiral-duct separating element operating by centrifugal action and gravity for classifying, preparing, rearranging and delivering a plurality of components at predetermined positions in the flow stream, and as a continuation of said spiral duct a walled transformation chamber having partitions in selected immersed positions thereby adapted to form separate flow channels to receive respectively the classified components in their aforesaid flow positions and with their efiective entrance areas selectively proportioned to the expected volumes of the components; and passages therebeyond arranged a to selected ones of such flow channels to join in confluence en route to the decanter thereby to conduct a combination of components into predetermined positions in the decanter.

7. An apparatus as in claim 6 and wherein the subdividing partitions in said transformation chamber are provided with adjustably shiftable vanes at the entrance to such channels, and exteriorly accessible means to adjust each of said vanes to vary the areas of one or more channel entrances to accord with the expected volumes of components.

8. Apparatus as in claim 6 and wherein there is included in the closed duct flow series, in advance of the spiral-duct separating element, a mixing element comprising a closed housing containing a perforated screen member and a mechanically operated wiper member moving in close proximity to the said screen member whereby the emulsions and lighter masses in the flow which constitute a complex component are, by the action of the screen and wiper elements, brought into contact one with another and are merged so as to form a single simple component suitable for separation by the action of said spiralduct separating element.

9. Apparatus as in claim 6 and wherein the spiral duct of said spiral-duct separating element has its walls disposed progressively to modify its sectional area whereby to provide a varying intensity of preparatory erosive action to meet the varying requirements and thereby obtain optimum preparation.

10. Apparatus for continuously separating a flowing mixture of separable liquid components of differing gravity and viscosity in which is included a decanter and in advance thereof a separating element for (l) classifying, (2) preparing and positioning and (3) withdrawing the several components, said separating element comprising (a) a helical duct member for classifying the flow, (b) a spiral duct member for preparing and positioning the components in the flow and (c) a flow dividing member for withdrawing the components so positioned; said helical duct member consisting of an axial core, and surrounding it a helical annular wall perpendicular to the axis of the core, which wall, with the outer and inner closure walls, forms a helical duct of which a first section composed of a number of convolutions of an initial group is closed and adapted to impose whirling and centrifugal classifying motions on the flow therethrough, followed by a second or flow-transfer section of which the convolutions are open in being formed with successive take-off mouths and. being connected liquid-tightly to said spiral duct member and being adapted to skim off from the whirling flow and deliver into said spiral duct member first the heavier liquid component to flow in contact with the concave side of the spiral partition wall of the said spiral duct member and thereafter the lighter liquid components; the duct in the said transfer section having a helical-spiral inner closure Wall constructed and arranged to decrease progressively and proportionately the area of the duct beyond each successive take-off mouth thereby to maintain such aforesaid flow speed and whirl and classifying action as the flow is currently delivered from said transfer section into the spiral duct member for preparation and positioning of the components in the flow; said spiral duct member consisting of a plurality of convolutions of a spirally disposed partition wall and cover plates to which its edges are attached so as to form a continuous spiral duct section beginning at and connected liquid tightly to the withdrawal mouths of the preceding helical duct member, followedby a walled tangential flow section connected liquidtightly to the succeeding flow-dividing member, whereby in said spiral duct member the several components, received fromthe helical ductmemher in determined sequence: and placement, are prepared by the centrifugal action of the flow while concurrently, under such centrifugal action combined with the action of the force of gravity; the said components are positioned in the flo'w for delivery to and withdrawal by the flow dividing member; and said flow dividing member consisting of a walled flow duct connected liquid tightly to the tangential section of the preceding spiral duct member and having partitions dividing it into separate channels formed with receiving mouths sized, shaped and positioned to receive the components to be withdrawn, in their expected position and volume, thereby to forward the components so withdrawn through the separate connections each in desired volume to desired disposal.

11. The apparatus as in claim 10 and wherein the subdividing partitions in the flow dividing member of the said separating element are constructed with movable vanes at the entrances to the said channels, and exteriorly accessible means to adjust said vanes to vary the channel entrances to accord with the expected volume of components to be withdrawn.

12. Apparatus as in claim 10 and wherein the spiral duct member of the said separating element has its walls disposed to modify progressively its sectional area whereby to provide a varying intensity of preparatory erosive action upon the mixed components to meet varying practical requirements and thereby obtain optimum preparation.

13. Apparatus as in claim 3 and wherein is a flow circulating pump and in tandem with such flow circulating pump and in advance of the aforesaid separating element a mixing element comprising a housing containing a perforated screen member and a mechanically operated wiper member moving in close proximity to the said screen member, whereby the emulsions and lighter masses in the flow which constitute a complex component are, by the action of said screen and wiper members, brought into contact one with another and merged thereby to form a single simple component suitable for separation by the action of the said separating element.

14. Apparatus as in claim 3 and wherein the said passages beyond the walled transformation chamber are fitted with means for controlling the relative resistance to flow therethrough whereby the velocity and volume of flow in the several passages is adjustably predetermined thereby to control the volume of flow to and through the decanter.

15. Apparatus as in claim 3 and wherein one of the said passages beyond the walled transformation chamber is connected to a storage vessel other than the decanter, and wherein the several passages are fitted with means for adjusting the relative resistance to flow therethrough whereby the velocity and volume of flow in the several passages is variably adjustable and a maximum quantity of the separated preponderant component is diverted to storage and is made currently available for process reuse and for recirculation in the separating apparatus.

CPI

16. Apparatus as in claim 3 and wherein for one of said passages arranged todivert its liquid from entering the decanter is an elevated overflow weir having its effective overflow level at a predetermined level well above the said transformation chamber and approximately near the decanter liquid top level, whereby, according to the relative liquid heads in said passage and the decanter respectively, the rate" of flow through said passage: and over said weir for diversion from the decanter is predetermined, and thereby the rate ofv flow into and from the decanter is predeterminable.

1'7. Apparatus for continuously separating from each other two separable components of a continuously flowing liquid mixture thereof supplied from an initial source in varying Volume of total flow and in varying proportions of such separable components, and wherein such components are of substantially difierent density and viscosity and comprise a minor volume of a more viscous component and a major volume of a more fluent component; said apparatus comprising, in combination with a decanter, a whirl-producing unit adapted continuously to effect the classifying, preparing and positioning of the respective components; a supply passage arranged to conduct the total mixture fiow into said unit; first and second withdrawal channels closely beyond and connected with said unit and adapted continuously and selectively to receive and withdraw therefrom the respective components,namely, the viscous first component modified by admixture with a stabilizing variable small volume of the fluent component and the remaining fluent second component free of the first component; said first withdrawal channel having an extension to deliver the modified first component into the decanter for further separation therein; and said second withdrawal channel having an extension to conduct said remaining second component to a place of re-use or other disposal, with means for continuously stabilizing the rate of total flow through said unit comprising an extension passage arranged to recirculate and deliver continuously from said second channel extension to said supply passage a portion of such withdrawn fluent component at a variable rate adequate to maintain substantially constant the volume rate and velocity of the total flow through said unit; and weir means between said second channel and its extension channel adapted to maintain for said second channel a continuous overflow of the fluent component therefrom at an elevation determined to correspond substantially with the desired operating surface level in the decanter; whereby there is maintained in said second channel a total resistance to fiow which is currently substantially equal to the total resistance to flow in such first channel, and whereby, through the resulting equalization of pressures in said first and second channels there are continuously maintained substantially constant rates of withdrawal of components from said unit through the respective withdrawal channels.

13. Apparatus for liquid separation as in claim 17 and wherein for controlling or correcting the rates of selective withdrawal of components into and through the respective first and second withdrawal channels to accord with prevailing conditions, there is provided a means for adjusting the elevation of the edge or weir over which the more fluent second component is overfiowed,

The following references are of record in the file of this patent:

UNITED STATES PATENTS Number Name Date 716,703 Gathmann Dec. 23, 1902 1,412,738 Heller Apr. 11, 1922 1,617,737 Averill Feb. 15, 1927 Number 10 Number Name Date Kerns et a1 Sept. 27, 1932 O'Toole June 13, 1933 Elliot Sept. 26, 1933 Hunter June 22, 1937 Wellman Feb. 24, 1942 Walker May 25, 1943 FOREIGN PATENTS Country Date Great Britain Aug. 21, 1919 France Oct. 14, 1935 Switzerland Oct. 1, 1919 

